CN104292181A - Method for concentrating acesulfame potassium mother liquor by adopting MVR system - Google Patents
Method for concentrating acesulfame potassium mother liquor by adopting MVR system Download PDFInfo
- Publication number
- CN104292181A CN104292181A CN201410501488.6A CN201410501488A CN104292181A CN 104292181 A CN104292181 A CN 104292181A CN 201410501488 A CN201410501488 A CN 201410501488A CN 104292181 A CN104292181 A CN 104292181A
- Authority
- CN
- China
- Prior art keywords
- acesulfame potassium
- mother liquor
- mixed liquor
- concentration
- concentrating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D291/00—Heterocyclic compounds containing rings having nitrogen, oxygen and sulfur atoms as the only ring hetero atoms
- C07D291/02—Heterocyclic compounds containing rings having nitrogen, oxygen and sulfur atoms as the only ring hetero atoms not condensed with other rings
- C07D291/06—Six-membered rings
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Saccharide Compounds (AREA)
- Seasonings (AREA)
Abstract
The invention relates to a method for concentrating acesulfame potassium mother liquor by adopting an MVR system. The method for concentrating the acesulfame potassium mother liquor by adopting the MVR system comprises the following steps: a, putting refined and saturated acesulfame potassium mother liquor into a cold sugar water tank by virtue of potential difference, cyclically mixing the mother liquor with cold sugar water, pumping the obtained mixed liquor into a preheater to be preheated, and then feeding the preheated mixed liquor into a heater; b, when temperature of mixed liquor is increased to 63-67 DEG C, feeding the mixed liquor into a primary concentration kettle at a uniform speed, circulating the mixed liquor between the heater and the primary concentration kettle, and controlling temperature of the mixed liquor to be 70-75 DEG C; c, after primary concentration reaction is carried out for 5.5-6.5 hours, pumping the primarily concentrated mixed liquor into a second concentration kettle to be subjected to secondary concentration, and controlling temperature to be 75-80 DEG C; and d, carrying out concentration reaction for 8.5-9.5 hours to generate acesulfame potassium crystal mixed liquor, crystallizing the acesulfame potassium crystal mixed liquor by virtue of a precooling kettle and a crystallizing machine, and centrifuging, so that an acesulfame potassium crude product is obtained. The method for concentrating the acesulfame potassium mother liquor by adopting the MVR system has the advantages that vapour consumption is greatly reduced, and production time is shortened, so that cost is reduced, and market competitiveness of the acesulfame potassium product is improved.
Description
Technical field
The invention belongs to foodstuff additive chemical technology field, relate to a kind of method that MVR system concentrates acesulfame potassium mother liquor.
Background technology
Acesulfame potassium is a kind of foodstuff additive, can increase food sweet taste, and mouthfeel is good, empty calory, has not metabolism in human body, does not absorb, and is the elderly, adiposis patient, sweeting agent that diabetic subject is desirable.After current acesulfame potassium production method is mainly and is utilized by saturated acesulfame potassium mother liquor steam heating concentrated, cool and centrifugally obtain thick product, then again with in and the raw sugar of cold syrup condensation that obtains of workshop section mix, enter recrystallization workshop section.This method needs two step condensations, consumes a large amount of steam, causes the waste of the energy, improves production cost.
Summary of the invention
The object of the invention is to solve the problem that in existing acesulfame potassium concentration process, steam consumption is excessive, provide a kind of MVR system to concentrate the method for acesulfame potassium mother liquor.
MVR system concentrates a method for acesulfame potassium mother liquor, it is characterized in that comprising the following steps:
A. acesulfame potassium is refined saturated mother liquor and put into cold syrup groove by potential difference, circulating with cold syrup mixes, and squeezes into preheater preheats, then send into well heater after mixing by pump;
B. when mixeding liquid temperature rises to 63 DEG C-67 DEG C, average rate sends into once concentration still, is circulated by mixed solution by forced circulation pump between well heater and once concentration still, and controlling mixeding liquid temperature is 70 DEG C ~ 75 DEG C;
After c once concentration reaction 5.5 ~ 6.5h terminates, material is squeezed into secondary concentration still and carry out secondary concentration, control still temperature 75 DEG C ~ 80 DEG C;
D., after the concentration response time of 8.5-9.5h, the acesulfame potassium crystallization mixture of generation, after precooling still, crystallizer crystallization, centrifugally obtains acesulfame potassium crude product.
On technique scheme basis, there is following further improvement project:
The steam produced in once concentration still is all recycled to well heater by vapour compressor and carries out second stage employ.
The invention has the advantages that and shorten the production time, save concentrated required steam, thus reduce production cost, improve production efficiency and product quality.
Accompanying drawing explanation
Fig. 1 is former concentrated acesulfame potassium mother liquor method flow diagram;
Fig. 2 is that MVR system concentrates acesulfame potassium mother liquor method flow diagram.
Embodiment
Embodiment 1
The cold syrup that in front workshop section and post produces enters syrup groove, then by pump by cold syrup 20m
3squeeze into cold syrup tempering tank, and put into 5m from refinement mother liquor header tank
3refinement mother liquor enters cold syrup tempering tank, ON cycle pump, by preheater circulating-heating, when mixeding liquid temperature rises to 65 DEG C, all squeezes into hot syrup groove (according to said method, repeating to join hot mixed solution), and by dnockout pump by preheated mixed solution (25m
3) squeeze into once concentration system and do bed material.ON cycle pump circulates, and opens vacuum pump evacuation, controls vacuum tightness-0.072Mpa, keeps once concentration still still temperature 73 DEG C.Open vapour compressor sprinkling system and oil piping system again, open compressor, load by little be adjusted to gradually maximum.By preheated mixed solution with 7.2m
3the speed of/h squeezes into once concentration system, the reaction times: 6.05h, enters syrup and mother liquor mixture 68.6m altogether
3.After once concentration reaction terminates, secondary concentration system all squeezed into by material, by the hydronics of secondary concentration, carries out secondary concentration, controls secondary concentration still still temperature 78 DEG C; The secondary concentration end time is: 3.15h.Before and after through the concentration response time of 9.2h, the acesulfame potassium crystallization mixture of generation, after precooling still, crystallizer crystallization, centrifugally obtains 7.8T acesulfame potassium crude product.In concentration process, the phlegma 58.2m of extraction
3whole Hui Qian workshop sections production line uses.
Embodiment 2
The cold syrup that in front workshop section and post produces enters syrup groove, then by pump by cold syrup 20m
3squeeze into cold syrup tempering tank, and put into 5m from refinement mother liquor header tank
3refinement mother liquor enters cold syrup tempering tank, ON cycle pump, by preheater circulating-heating, when mixeding liquid temperature rises to 67 DEG C, all squeezes into hot syrup groove (according to said method, repeating to join hot mixed solution), and by dnockout pump by preheated mixed solution (25m
3) squeeze into once concentration system and do bed material.ON cycle pump circulates, and opens vacuum pump evacuation, controls vacuum tightness-0.072Mpa, keeps once concentration still still temperature 72 DEG C.Open vapour compressor sprinkling system and oil piping system again, open compressor, load by little be adjusted to gradually maximum.By preheated mixed solution with 7.4m
3the speed of/h squeezes into once concentration system, the reaction times: 5.95h, enters syrup and mother liquor mixture 69.1m altogether
3.After once concentration reaction terminates, secondary concentration system all squeezed into by material, by the hydronics of secondary concentration, carries out secondary concentration, controls secondary concentration still still temperature 76 DEG C; The secondary concentration end time is: 3.15h.Before and after through the concentration response time of 9.1h, the acesulfame potassium crystallization mixture of generation, after precooling still, crystallizer crystallization, centrifugally obtains 8.2T acesulfame potassium crude product.In concentration process, the phlegma 59.1m of extraction
3whole Hui Qian workshop sections production line uses.
Two kinds of production method parameter lookup table
From synopsis, novel method of the present invention improves production capacity, substantially reduces the product cycle, improves steam utilization and productive rate, serves substantial effect to production.
Claims (2)
1. MVR system concentrates a method for acesulfame potassium mother liquor, it is characterized in that comprising the following steps:
A. acesulfame potassium is refined saturated mother liquor and put into cold syrup groove by potential difference, circulating with cold syrup mixes, and squeezes into preheater preheats, then send into well heater after mixing;
B. when mixeding liquid temperature rises to 63 DEG C-67 DEG C, average rate sends into once concentration still, is circulated by mixed solution between well heater and once concentration still, and controlling mixeding liquid temperature is 70 DEG C ~ 75 DEG C;
C., after once concentration reaction 5.5 ~ 6.5h terminates, material is squeezed into secondary concentration still and carry out secondary concentration, control temperature is 75 DEG C ~ 80 DEG C;
D. through the concentration response time of 8.5-9.5h, the acesulfame potassium crystallization mixture of generation, after precooling still, crystallizer crystallization, centrifugally obtains acesulfame potassium crude product.
2. a kind of MVR system according to claim 1 concentrates the method for acesulfame potassium mother liquor, it is characterized in that, the steam produced in once concentration still is all recycled to well heater by vapour compressor and carries out second stage employ.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410501488.6A CN104292181B (en) | 2014-09-27 | 2014-09-27 | A kind of MVR system concentrates the method for acesulfame potassium mother solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410501488.6A CN104292181B (en) | 2014-09-27 | 2014-09-27 | A kind of MVR system concentrates the method for acesulfame potassium mother solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104292181A true CN104292181A (en) | 2015-01-21 |
| CN104292181B CN104292181B (en) | 2016-10-26 |
Family
ID=52312170
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410501488.6A Active CN104292181B (en) | 2014-09-27 | 2014-09-27 | A kind of MVR system concentrates the method for acesulfame potassium mother solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104292181B (en) |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10023546B2 (en) | 2016-09-21 | 2018-07-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029998B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10030000B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029999B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| CN109045744A (en) * | 2018-08-30 | 2018-12-21 | 山东亚邦化工科技有限公司 | The method and apparatus for preparing acesulfame potassium crystallization of continuous-stable |
| CN109078359A (en) * | 2018-08-30 | 2018-12-25 | 山东亚邦化工科技有限公司 | A kind of technique and device for acesulfame potassium sulfonation hydrolysis liquid continuous extration |
| CN109369572A (en) * | 2018-10-25 | 2019-02-22 | 苏州浩波科技股份有限公司 | A kind of purifying process of acesulfame potassium |
| CN109593071A (en) * | 2018-12-10 | 2019-04-09 | 安徽金禾实业股份有限公司 | A kind of continuous controllable acesulfame potassium recrystallization centrifugal device and method |
| CN110818654A (en) * | 2019-12-20 | 2020-02-21 | 安徽金禾实业股份有限公司 | Optimized acesulfame crystallization method |
| CN110846443A (en) * | 2019-11-16 | 2020-02-28 | 安徽金禾实业股份有限公司 | Method for optimizing crystallization by back extraction of acesulfame-K syrup |
| CN112110875A (en) * | 2020-09-26 | 2020-12-22 | 安徽金禾实业股份有限公司 | Preheating method for mother liquor in heavy material boiling section |
| CN112221179A (en) * | 2020-09-26 | 2021-01-15 | 安徽金禾实业股份有限公司 | Spraying method of secondary concentration kettle in acesulfame potassium production |
| CN112480033A (en) * | 2020-11-30 | 2021-03-12 | 安徽金禾实业股份有限公司 | Method for two-stage continuous concentration of sugar water in acesulfame potassium production |
| USRE48464E1 (en) | 2012-06-08 | 2021-03-16 | Celanese Sales Germany Gmbh | Process for producing acesulfame potassium |
| CN112592325A (en) * | 2020-11-28 | 2021-04-02 | 安徽金禾实业股份有限公司 | Method and device for recovering potassium salt in acesulfame potassium crystallization waste liquid |
| CN115677620A (en) * | 2022-11-17 | 2023-02-03 | 安徽金禾实业股份有限公司 | Method for treating coarse mother liquor in acesulfame potassium production |
| CN115710236A (en) * | 2022-11-17 | 2023-02-24 | 安徽金禾实业股份有限公司 | Method for continuously concentrating sugar water in acesulfame potassium production |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4607100A (en) * | 1984-03-22 | 1986-08-19 | Hoechst Aktiengesellschaft | Process for the preparation of 6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide and its non-toxic salts |
| CN86105339A (en) * | 1985-09-03 | 1987-04-08 | 赫彻斯特股份公司 | 6-methyl-3,4-dihydro-1,2,3-oxygen thia azine hexamethylene-4-ketone 2, the preparation of 2-dioxide and method of purification |
| US5744010A (en) * | 1992-03-17 | 1998-04-28 | Hoechst Aktiengesellschaft | Process for the preparation of the non-toxic salts of 6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide and arrangement for carrying out this process |
| WO1999064444A1 (en) * | 1998-06-05 | 1999-12-16 | Holland Sweetener Company V.O.F. | Preparation of an organic salt of aspartame with acesulfam h |
| CN1323792A (en) * | 2001-05-15 | 2001-11-28 | 张家港浩波化学品有限公司 | Synthesis of acetyl sulfanilic acid and its potassium salt |
| US20020160091A1 (en) * | 2001-04-26 | 2002-10-31 | Andreas Burgard | Acesulfame salt, process for its preparation and its use |
| CN1927849A (en) * | 2006-09-24 | 2007-03-14 | 张家港浩波化学品有限公司 | Hydrolysis process of synthesizing potassium acetylsulfamilate and special device for the same |
| CN101124981A (en) * | 2007-09-12 | 2008-02-20 | 安徽金禾实业股份有限公司 | Concentrating method and device in acesulfame potassium production |
| CN102336647A (en) * | 2011-07-06 | 2012-02-01 | 滁州学院 | Application of AK sugar crystal mother liquor and method for preparing sylvite by crystal mother liquor |
| CN102380226A (en) * | 2011-09-07 | 2012-03-21 | 安徽金禾实业股份有限公司 | Acesulfame sugar water concentration method |
| US20130331565A1 (en) * | 2012-06-08 | 2013-12-12 | Nutrinova Nutrition Specialties & Food Ingredients | Process for Producing Acesulfame Potassium |
| CN103588728A (en) * | 2013-11-01 | 2014-02-19 | 安徽金禾实业股份有限公司 | Neutralization direct crystallization production technology of acesulfame potassium |
-
2014
- 2014-09-27 CN CN201410501488.6A patent/CN104292181B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4607100A (en) * | 1984-03-22 | 1986-08-19 | Hoechst Aktiengesellschaft | Process for the preparation of 6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide and its non-toxic salts |
| CN86105339A (en) * | 1985-09-03 | 1987-04-08 | 赫彻斯特股份公司 | 6-methyl-3,4-dihydro-1,2,3-oxygen thia azine hexamethylene-4-ketone 2, the preparation of 2-dioxide and method of purification |
| US5744010A (en) * | 1992-03-17 | 1998-04-28 | Hoechst Aktiengesellschaft | Process for the preparation of the non-toxic salts of 6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide and arrangement for carrying out this process |
| WO1999064444A1 (en) * | 1998-06-05 | 1999-12-16 | Holland Sweetener Company V.O.F. | Preparation of an organic salt of aspartame with acesulfam h |
| US20020160091A1 (en) * | 2001-04-26 | 2002-10-31 | Andreas Burgard | Acesulfame salt, process for its preparation and its use |
| CN1323792A (en) * | 2001-05-15 | 2001-11-28 | 张家港浩波化学品有限公司 | Synthesis of acetyl sulfanilic acid and its potassium salt |
| CN1927849A (en) * | 2006-09-24 | 2007-03-14 | 张家港浩波化学品有限公司 | Hydrolysis process of synthesizing potassium acetylsulfamilate and special device for the same |
| CN101124981A (en) * | 2007-09-12 | 2008-02-20 | 安徽金禾实业股份有限公司 | Concentrating method and device in acesulfame potassium production |
| CN102336647A (en) * | 2011-07-06 | 2012-02-01 | 滁州学院 | Application of AK sugar crystal mother liquor and method for preparing sylvite by crystal mother liquor |
| CN102380226A (en) * | 2011-09-07 | 2012-03-21 | 安徽金禾实业股份有限公司 | Acesulfame sugar water concentration method |
| US20130331565A1 (en) * | 2012-06-08 | 2013-12-12 | Nutrinova Nutrition Specialties & Food Ingredients | Process for Producing Acesulfame Potassium |
| CN103588728A (en) * | 2013-11-01 | 2014-02-19 | 安徽金禾实业股份有限公司 | Neutralization direct crystallization production technology of acesulfame potassium |
Non-Patent Citations (3)
| Title |
|---|
| 薛连海 等: "安赛蜜生产控制分析方法的改进", 《滁州学院学报》 * |
| 闫福安 等: "甜味剂安赛蜜的合成工艺研究", 《食品工业科技》 * |
| 黄林峰: "安赛蜜工厂工艺流程设计探讨", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
Cited By (39)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| USRE48464E1 (en) | 2012-06-08 | 2021-03-16 | Celanese Sales Germany Gmbh | Process for producing acesulfame potassium |
| US10759770B2 (en) | 2016-09-21 | 2020-09-01 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10961207B2 (en) | 2016-09-21 | 2021-03-30 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029999B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11731948B2 (en) | 2016-09-21 | 2023-08-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10781190B2 (en) | 2016-09-21 | 2020-09-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10208004B2 (en) | 2016-09-21 | 2019-02-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11724993B2 (en) | 2016-09-21 | 2023-08-15 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10227316B2 (en) | 2016-09-21 | 2019-03-12 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10759771B2 (en) | 2016-09-21 | 2020-09-01 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10233163B2 (en) | 2016-09-21 | 2019-03-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11718594B2 (en) | 2016-09-21 | 2023-08-08 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10975047B2 (en) | 2016-09-21 | 2021-04-13 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10030000B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590095B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590097B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590098B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590096B2 (en) | 2016-09-21 | 2020-03-17 | Celenese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10023546B2 (en) | 2016-09-21 | 2018-07-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10233164B2 (en) | 2016-09-21 | 2019-03-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11724994B2 (en) | 2016-09-21 | 2023-08-15 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029998B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10954204B2 (en) | 2016-09-21 | 2021-03-23 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10954203B2 (en) | 2016-09-21 | 2021-03-23 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10781191B2 (en) | 2016-09-21 | 2020-09-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| CN109045744B (en) * | 2018-08-30 | 2021-04-27 | 山东亚邦化工科技有限公司 | Method and device for continuously and stably preparing acesulfame potassium crystals |
| CN109045744A (en) * | 2018-08-30 | 2018-12-21 | 山东亚邦化工科技有限公司 | The method and apparatus for preparing acesulfame potassium crystallization of continuous-stable |
| CN109078359B (en) * | 2018-08-30 | 2020-11-06 | 山东亚邦化工科技有限公司 | Process and device for continuous extraction of acesulfame potassium sulfonated hydrolysate |
| CN109078359A (en) * | 2018-08-30 | 2018-12-25 | 山东亚邦化工科技有限公司 | A kind of technique and device for acesulfame potassium sulfonation hydrolysis liquid continuous extration |
| CN109369572A (en) * | 2018-10-25 | 2019-02-22 | 苏州浩波科技股份有限公司 | A kind of purifying process of acesulfame potassium |
| CN109593071A (en) * | 2018-12-10 | 2019-04-09 | 安徽金禾实业股份有限公司 | A kind of continuous controllable acesulfame potassium recrystallization centrifugal device and method |
| CN110846443A (en) * | 2019-11-16 | 2020-02-28 | 安徽金禾实业股份有限公司 | Method for optimizing crystallization by back extraction of acesulfame-K syrup |
| CN110818654A (en) * | 2019-12-20 | 2020-02-21 | 安徽金禾实业股份有限公司 | Optimized acesulfame crystallization method |
| CN112221179A (en) * | 2020-09-26 | 2021-01-15 | 安徽金禾实业股份有限公司 | Spraying method of secondary concentration kettle in acesulfame potassium production |
| CN112110875A (en) * | 2020-09-26 | 2020-12-22 | 安徽金禾实业股份有限公司 | Preheating method for mother liquor in heavy material boiling section |
| CN112592325A (en) * | 2020-11-28 | 2021-04-02 | 安徽金禾实业股份有限公司 | Method and device for recovering potassium salt in acesulfame potassium crystallization waste liquid |
| CN112480033A (en) * | 2020-11-30 | 2021-03-12 | 安徽金禾实业股份有限公司 | Method for two-stage continuous concentration of sugar water in acesulfame potassium production |
| CN115710236A (en) * | 2022-11-17 | 2023-02-24 | 安徽金禾实业股份有限公司 | Method for continuously concentrating sugar water in acesulfame potassium production |
| CN115677620A (en) * | 2022-11-17 | 2023-02-03 | 安徽金禾实业股份有限公司 | Method for treating coarse mother liquor in acesulfame potassium production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104292181B (en) | 2016-10-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104292181A (en) | Method for concentrating acesulfame potassium mother liquor by adopting MVR system | |
| CN104261429B (en) | The continuous triple effect falling film concentration of ammonium chloride, vacuum crystallization system and method in a kind of double decomposition Production of Potassium Nitrate | |
| CN101156675A (en) | Glutamic acid abstraction technics combining rotation crystal | |
| CN104261438B (en) | A kind of system and method for continous way preparing potassium nitrate by means of double decomposition | |
| CN104261435B (en) | A kind of double decomposition potassium nitrate crystal system and crystallization processes | |
| CN104261437B (en) | A kind ofly produce with liquid ammonium nitrate the continous way Production of Potassium Nitrate system combining | |
| CN104310443B (en) | A kind ofly produce with liquid ammonium nitrate the continous way Production of Potassium Nitrate system and the production method that combine | |
| CN102992353A (en) | Technology for producing industrial-grade ammonium chloride by quadruple-effect evaporation heat method | |
| CN106117038A (en) | A kind of technique using nisin waste water to produce calcium lactate | |
| CN104310442B (en) | Concentrated, the vacuum crystallization system of the continuous triple effect of ammonium chloride pump circulation and technique in a kind of double decomposition Production of Potassium Nitrate | |
| CN104310441B (en) | Reaction heat utilization system and method in a kind of potassium nitrate combined producting ammonium chloride production | |
| CN103535492A (en) | Production method of rock candy | |
| CN106244648A (en) | A kind of method of corn starch milk preparation fruit glucose syrup | |
| CN101255120B (en) | Novel technique for extracting glutaminic acid | |
| CN104310440B (en) | A kind of system and method for continous way preparing potassium nitrate by means of double decomposition | |
| CN104261436B (en) | A kind of system and method for continous way preparing potassium nitrate by means of double decomposition | |
| CN104118958A (en) | Fumaric acid wastewater recovery treatment technique | |
| CN206167974U (en) | Continuous single -action vacuum evaporation crystal system | |
| CN100488591C (en) | Evaporative crystallization technique for solution of temperature sensitive crystalline materiel | |
| CN101103803B (en) | Glutamic acid crystalloblastic technology | |
| CN207016797U (en) | A kind of enrichment facility of liquid glucose energy-conserving and environment-protective | |
| CN104310438B (en) | A kind of system and method for continous way preparing potassium nitrate by means of double decomposition | |
| CN207734641U (en) | A kind of crystallizing tank of energy uniform decrease in temperature | |
| CN205925037U (en) | Sulfate process titanium dioxide titaniferous solution's enrichment facility | |
| CN104195590A (en) | Treatment method of gluconate crystallization mother liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |